EP0056487A2 - Procédé d'hydrogénation du charbon - Google Patents

Procédé d'hydrogénation du charbon Download PDF

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Publication number
EP0056487A2
EP0056487A2 EP81110725A EP81110725A EP0056487A2 EP 0056487 A2 EP0056487 A2 EP 0056487A2 EP 81110725 A EP81110725 A EP 81110725A EP 81110725 A EP81110725 A EP 81110725A EP 0056487 A2 EP0056487 A2 EP 0056487A2
Authority
EP
European Patent Office
Prior art keywords
heat
coal
hydrogenation
gas
gases
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP81110725A
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German (de)
English (en)
Other versions
EP0056487A3 (en
EP0056487B1 (fr
Inventor
Helmut Dr. Romberg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Saarbergwerke AG
Original Assignee
BASF SE
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of EP0056487A2 publication Critical patent/EP0056487A2/fr
Publication of EP0056487A3 publication Critical patent/EP0056487A3/de
Application granted granted Critical
Publication of EP0056487B1 publication Critical patent/EP0056487B1/fr
Expired legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/083—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts in the presence of a solvent

Definitions

  • the direct heat exchange between Christsdäm p fen and coal slurry would provide benefits.
  • the mixing section required for direct heat exchange is less sensitive to distribution problems of the two-phase mixture, and there is no risk of cracking on overheated heat exchanger surfaces.
  • the use of hydrogen as an essential component of the heat transfer gas also guarantees that the coal pulp is always heated in the presence of hydrogen.
  • Direct heat exchange has also already been carried out in one step or over a limited temperature range in a countercurrent apparatus. In both cases, some of the vaporous reaction products condense out in the pulp; this limits the application of the principle of direct heat exchange to a relatively high temperature level. Extensive heat recovery through direct exchange is not possible in this way.
  • the gases and vapors flowing from the reaction were cooled to a temperature not below 350 ° C., preferably to a temperature between 380 and 440 ° C., in particular 390 to 410 ° C., in a first mixing stage. Then high-boiling oils are separated in an intermediate separator. In order to achieve this temperature in the intermediate separator, a preheating section at lower temperatures is required, in which the coal slurry is preheated. With direct heat exchange, the reaction gas is cooled to temperatures lower than 350 ° C. When cooling below 350 ° C, however, an excessive amount of the reaction products would fail here and be fed back to the reactor with the coal pulp.
  • reaction products in the paste and in the reaction zone is prevented by the reaction products being previously removed from the reaction gases in a cold separator at about room temperature.
  • the remaining gas, freed from the oil vapor, is then heated in countercurrent with the product-laden gas flowing to the cold separator in a heat exchanger, the gas flowing to the cold separator being cooled.
  • This heated gas, freed from the product can now serve as a heat carrier and supply the necessary heat to the paste in a direct heat exchange. If additional heat is required to cover a peak demand, the product-free gas can be heated with this external heat without the heat-transferring surfaces cracking or otherwise occupy themselves with carbon. '
  • the advantage of the procedure according to the invention consists essentially in the fact that only clean gases enter the heat exchanger for the external heat supply, while the coal pulp is heated by direct heating in multiphase mixing sections which are considerably simpler in terms of equipment and thus cheaper, without the risk of cracking Individual pipes are laid and there is overheating on the heat exchanger surfaces.
  • the coal pulp is always heated in the presence of hydrogen.
  • the effect of the countercurrent principle can largely be achieved by suitable selection of the number of stages of direct heating.
  • the mixing stages which are operated at temperatures below 400 ° C. and to which the heat is supplied by gas from which the product has already condensed, can also be designed as countercurrent apparatuses in order to achieve even better heat utilization.
  • the advantage of the process according to the invention is that the coal pulp, which is difficult to treat, is directly mixed with gases from the process onto the reactor is brought to the temperature, the external heat supply, in contrast to a single-stage circuit, can usually be omitted entirely or at least kept significantly smaller.
  • the multi-stage direct mixing is made possible by separating the gas from the product of value after the first mixing section, so that no product can fail in the colder mixing stages. It is only through the multi-stage direct mixing that the known advantages of direct heating over indirect heating in tubular bilge heat exchangers can be optimally used: With direct heating in a mixing section, the problem of distributing the coal slurry in the heat exchanger can be solved much better, especially with very large appliances with indirect heat exchange, in which dead zones can easily form, which are harmful to the product and occupy the exchange surfaces. This is the main advantage compared to indirect heat exchange in counterflow. Much simpler apparatuses than shell-and-tube heat exchangers can be used as mixing sections for direct heat exchange, especially at high pressure.
  • Direct mixing makes it possible to use coal that has not been pre-dried.
  • the expelled water vapor and other low boilers are not passed through the reactor, but are discharged directly via a cold separator.
  • the coal Even when predried, the coal still contains a significant proportion of water, which increases the reaction pressure as steam in the reactor. In the case of direct heating, this amount of water is also removed together with the volatile constituents of the coal and of the grinding oil in front of the reactor, so that the reaction pressure can be lower by the partial pressures of these low boilers.
  • the slurry is fed into the reactor with the pump (6).
  • the hydrogen required for the hydrogenation namely fresh hydrogen and the process-related circulating hydrogen, enters the reactor (21).
  • This gas stream is heated with heat recovery in the heat exchangers (19) and (15).
  • the heat exchanger (12) is additionally provided in order to be able to supply any external heat that may be required.
  • the reactor gas separated in the intermediate separator (7) is cooled in the heat exchangers (14) and (15) in a heat network and brought close to room temperature; the cold separator oil condenses out and can be separated in the cold separator (16) (stream (17)).
  • the product-free gas which is heated in the heat exchanger (14) with heat recovery and - if there is a need for external heat - in the heat exchanger (11), reaches the mixing section (2), where it is mixed with the coal pulp entering the system (1).
  • the mash is heated.
  • the coal slurry (1) in step is preheated (2) of 100 ° C to 230 ° C, the heating then takes place in the other mixer stage (8) to the necessary temperature of 400 0 C.
  • the heating network which conditions appropriate exchange areas, the need for external heat can be brought to zero.
  • the gas flow passed through the exchange stage (2) is to be increased for better heat recovery, the gas flow can be removed behind the separator (22). which is to be conducted for gas purification, a partial stream (20) is branched off and pumped to stage (2) with the aid of the circulating gas compressor (18) via (14) and (11).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Paper (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
EP81110725A 1981-01-20 1981-12-23 Procédé d'hydrogénation du charbon Expired EP0056487B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3101598 1981-01-20
DE19813101598 DE3101598A1 (de) 1981-01-20 1981-01-20 Verfahren zum hydrieren von kohle

Publications (3)

Publication Number Publication Date
EP0056487A2 true EP0056487A2 (fr) 1982-07-28
EP0056487A3 EP0056487A3 (en) 1983-06-22
EP0056487B1 EP0056487B1 (fr) 1985-11-21

Family

ID=6122930

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81110725A Expired EP0056487B1 (fr) 1981-01-20 1981-12-23 Procédé d'hydrogénation du charbon

Country Status (3)

Country Link
US (1) US4468315A (fr)
EP (1) EP0056487B1 (fr)
DE (2) DE3101598A1 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3246609A1 (de) * 1982-12-16 1984-06-20 GfK Gesellschaft für Kohleverflüssigung mbH, 6600 Saarbrücken Verfahren zum hydrieren von kohle
DE3438330C2 (de) * 1983-11-05 1987-04-30 GfK Gesellschaft für Kohleverflüssigung mbH, 6600 Saarbrücken Verfahren zum Verflüssigen von Kohle
DE3585485D1 (de) * 1984-09-13 1992-04-09 Ruhrkohle Ag Verfahren zur prozesseinstellung mit waermerueckgewinnung fuer die sumpfphasehydrierung mit integrierter gasphasehydrierung.
CN105295990B (zh) * 2015-10-23 2017-10-03 北京中科诚毅科技发展有限公司 一种浆态床加氢工艺的原料预处理的方法及其设计方法和用途

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1876009A (en) * 1926-02-06 1932-09-06 Standard Ig Co Conversion of solid fuels and products derived therefrom or other carbonaceous materials into valuable products
DE669660C (de) * 1934-07-07 1938-12-31 I G Farbenindustrie Akt Ges Verfahren zur Herstellung von fluessigen Kohlenwasserstoffoelen durch Druckhydrierung fester kohlenstoffhaltiger Stoffe
US4113602A (en) * 1976-06-08 1978-09-12 Exxon Research & Engineering Co. Integrated process for the production of hydrocarbons from coal or the like in which fines from gasifier are coked with heavy hydrocarbon oil
DE2654635B2 (de) * 1976-12-02 1979-07-12 Ludwig Dr. 6703 Limburgerhof Raichle Verfahren zur kontinuierlichen Herstellung von Kohlenwasserstoffölen aus Kohle durch spaltende Druckhydrierung
DE2711105C2 (de) * 1977-03-15 1984-05-24 Saarbergwerke AG, 6600 Saarbrücken Verfahren zur Umwandlung von Kohle in unter Normalbedingungen flüssige Kohlenwasserstoffe
US4222844A (en) * 1978-05-08 1980-09-16 Exxon Research & Engineering Co. Use of once-through treat gas to remove the heat of reaction in solvent hydrogenation processes
US4189375A (en) * 1978-12-13 1980-02-19 Gulf Oil Corporation Coal liquefaction process utilizing selective heat addition
US4297200A (en) * 1980-01-18 1981-10-27 Briley Patrick B Method for hydroconversion of solid carbonaceous materials
DE3042984C2 (de) * 1980-11-14 1986-06-26 Saarbergwerke AG, 6600 Saarbrücken Verfahren zum Hydrieren von Kohle

Also Published As

Publication number Publication date
US4468315A (en) 1984-08-28
EP0056487A3 (en) 1983-06-22
EP0056487B1 (fr) 1985-11-21
DE3173032D1 (en) 1986-01-02
DE3101598A1 (de) 1982-08-26

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